Method for creating white alkanes from non-petroleum renewable sources

ABSTRACT

The present invention describes a method to produce high purity hydrocarbon materials from renewable sources. The produced materials are chemically indistinguishable from highly refined mineral oils and/or synthetic hydrocarbons. These renewable hydrocarbon materials can be used as a drop-in replacement for mineral and synthetic hydrocarbon base oils, process fluids, white oils in products such as lubricants, rubber, personal care, pharma.

This application is based upon and claims priority from U.S. Provisionalapplication Ser. No. 63/310,454, filed Feb. 15, 2022, which isincorporated herein by reference.

BACKGROUND OF THE INVENTION Field of the Invention

Applicants' invention relates to a method for producing renewablehydrocarbon fluids that have properties similar to white oil but thatare derived from non-petroleum sources. Further, it relates to thepurified fluids derived from the method.

Background Information

The American Petroleum Institute (“API”) has categorized base oils intofive (5) categories, or groups—Groups I-V (API 1509, Appendix E). Baseoils often are used as lubricants, which frequently have variousadditives mixed with the base oil. If a base oil is classified as GroupI-III, that base oil will be composed of crude petroleum oil that hasbeen treated. As a general statement, any oil-based lubricant will becomposed of 80-99% of base oil. In contrast, Groups IV and V are notderived directly from crude oil.

Certain physical properties are used to describe the characteristics ofthe base oils. “Viscosity” is a measure of its resistance to deformationat a given flow rate. Viscosity is usually measured in centistokes (cSt)or in other units such as Saybolt units. Viscosity can be used to definebase oil grade and is determined by various methods, such as gravityflow capillary viscometer. The “viscosity-index” (“VI”) relates to howmuch the viscosity changes with temperature—how much it thins out athigher temperatures and thickens at lower temperatures, and isdetermined by the variance in viscosity between 40° C. and 100° C.“Specific gravity” defines the density of oil relative to water and ismeasured by a hydrometer. The base oils' “flash point” describes itshigh-temperature, flammability property, and is the temperature at whicha flash surface flame occurs. Finally, “pour point” defines the lowesttemperature at which an oil is observed to flow by gravity in aspecified lab test. Specifically, the pour point is 3 degrees C. (5degrees F.) above the temperature at which the oil shows no movementwhen a lab sample container is held horizontally for 5 seconds.

Group I base oils are refined from petroleum crude oil, but are theleast refined base oil. Group I base oils are solvent-refined, which isa simpler refining process, and Group I base oils typically range fromamber to golden brown in color due to the Sulphur, nitrogen and ringstructures remaining in the oil. Two main characteristics of Group Ibase oils are that they are composed of one or both of: less than 90%saturates and/or greater than 0.03% sulfur. Group I base oils have a VIrange of 80 to 120.

Group II base oils are defined as being, both, more than 90% saturatesand less than 0.03% sulfur. They are created by using a hydrotreatingprocess to replace the traditional solvent-refining process, which is amore complex process than what is used for Group I base oils. Hydrogengas is used to remove undesirable components from the crude oil. Thisresults in a clear, clearer than Group I base oils, and colorless baseoil with very few Sulphur, nitrogen or ring structures. All thehydrocarbon molecules of Group II base oils are saturated, giving thembetter antioxidation properties. The VI of Group II base oils indexranges from 80 to 120, but is typically above 100.

Group III base oils are greater than 90 percent saturates, less than0.03 percent sulfur. These oils are refined using a hydrogen gas processto clean up the crude oil even more than Group II base oils, andgenerally are severely hydrocracked (higher pressure and heat). Thislonger process is designed to achieve a purer base oil. The resultingbase oil is clear and colorless. Group III base oils are more resistantto oxidation than Group I oils. The VI of Group III base oils index isabove 120. Group III base oils are considered mineral oils by manytechnical people because they are derived directly from the refining ofcrude oil. However, they are considered synthetic base oils by otherpeople for marketing purposes due to the belief that the harsherhydrogen process has created new chemical oil structures that were notpresent before the process.

Group IV base oils are full synthetic (polyalphaolefin) oils.Polyalphaolefins (“PAO”) are made through a process called synthesizingusing pure chemicals created in a chemical plant as opposed to beingcreated by distillation and refining of crude oil. They have a muchbroader temperature range and are great for use in extreme coldconditions and high heat applications. PAOs have a VI of greater than120.

Group V base oils are classified as all other base oils that are notclassified as belonging in Groups I-IV. These base oils are at timesmixed with other base stocks to enhance the oil's properties. CommonGroup V base oils include naphthenic base oils, various syntheticesters, polyalkylene glycols (PAGs), phosphate esters, silicone,phosphate ester, polyolester, biolubes, and various other chemistriesfall into this group.

The terms base stocks and base oils are often used interchangeably, butthere are differences. A base stock is a single product, usually definedby its viscosity grade. A mixture of one or more base stocks in afinished lubricant is a base oil. A base oil is always defined in thecontext in the formulated lubricant. Base oil properties can varydepending on their API group.

Mineral oil can also be obtained as a distillation product made fromhighly refined, purified, distilled, and processed petroleum. It is aninert, chemically stable compound. Mineral oil is also known by theterms “paraffinum perliquidum” for light mineral oil and “paraffinumliquidum” or “paraffinum subliquidum” for somewhat more viscousvarieties. Various mineral oils are combinations of paraffins,naphthenes, and aromatic oils that are clear, colorless, oily, almosttasteless, water-insoluble liquid, usually of either a standard lightdensity (light mineral oil) or a standard heavy density (heavy mineraloil). Mineral oil is an inert, stable compound that is often used as aningredient used in baby lotions, cold creams, ointments, lubricants,cosmetics, moisturizers, laxatives, and many other cosmetic and personalcare products. Mineral oil is also used in the manufacture of some basicfoods. It is used as a binding agent, but can also be applied to grainslike wheat, rice, oats and barley to help keep dust from adhering to theproduct. Mineral oil is also an ingredient in some types of gummycandies to keep them from sticking together.

White oil is a mineral oil that is colorless, odorless, tastelessmineral oils, and is used especially in medicine and in pharmaceuticaland cosmetic preparations. White mineral oils are a highly refinedpetroleum mineral oil. White mineral oils mostly consist of saturatedhydrocarbons. Different methods of purifying are applied: hydrogenation,hydro-isomerization, or sulfur trioxide (SO₃), sulfuric acid, or oleumtreatment of petroleum products, or a combination of the above. Whitemineral oils are used in many applications in personal care, pharma,food industry (including lubricants), and many other applications wherenon-toxic oil with low biological activity and high stability isrequired.

White oil consists of a complex combination of hydrocarbons obtainedfrom the intensive treatment of a petroleum fraction with sulfuric acidand oleum, or by hydrogenation, or by a combination of hydrogenation andacid treatment. Additional washing and treating steps may be included inthe processing operation. It consists of saturated hydrocarbons havingcarbon numbers predominantly in the range of C15 through C50. The term“white oil” is a misnomer, in that white oils are clear, and tend to bewater white (Saybolt color +30), and meet guidelines established by theFood and Drug Administration (FDA) in the Code of Federal Regulations(CFR). 21 CFR 172.878 and 21 CFR 178.3620(a) They meet the purityrequirements of the European Pharmacopoeia (EuP), United StatesPharmacopoeia (USP), and Japanese Pharmacopoeia (JP). Moreover they arein compliance with the purity requirements of former monographs of theBP, DAB or French Codex. Typical properties of white oils include:density from 810-890 kg/m³ at 20° C. (using the standard test fordensity ASTM D-1298), viscosity from 3-240 cSt at 40° C. (using thestandard test for viscosity ASTM D-445), pour point from −18-+3° C.(using the standard test for pour point ASTM D-97), flash point from115-290° C. (using the standard test for flash point ASTM D-92). (Otherstandards and tests exist for these properties as well.)

Conventional methods using renewable materials are not “drop-in”replacement for mineral and synthetic PAO oil and produce products withinferior quality and hence are only suited to limited applications.Today, the renewable based alternatives for petroleum base oils, processfluids, and white oils are usually based on vegetable oils or productsderived from chemical modification of vegetable oils (for example,di-esters and polyol esters). These products possess reactive estergroups that negatively affect the properties of the final product. Hencethese materials often don't deliver the same performance as mineral oilsin conventional lubricating and other industrial applications.

SUMMARY OF THE INVENTION

The present invention includes the process of producing hydrocarbonmaterial from renewable sources that are not sourced from petroleum (orcrude oil) and meeting all or part of the technical requirements ofwhite mineral oil specifications (European (EuP), United States (USP),Japanese Pharmacopoeia (JP), former monographs of the BP, DAB or FrenchCodex). The present invention also includes producing the resultantsubstance using the method. The resulting substance is called a WhiteAlkanes, which is generally a liquid (some products are waxy) and haswhite oil-like characteristics.

As used herein, “White Alkane” or “White Alkanes” is the resultantproduct after subjecting renewable sources to the described processes,and where the White Alkanes are inert and have all or some of: specifiedfeed materials, carbon chains with a given range of numbers of carbonmolecules, viscosities in a given range, UV absorption, aromatics,color, readily carbonizable substances, improved pour points, improvedflash points, a clear (or generally clear) appearance, specificgravity/relative density, acidity/alkalinity, no, or virtually no,remaining sulfur compounds, where the ranges and requirements arefurther described herein.

The resulting White Alkanes come from polymerized vegetable oils ordimer fatty acids or similar materials containing hydrocarbon chains inC12-C100 range for use in various applications, including for personalcare products and lubricants. The method economically produces highpurity renewable base oils or hydrocarbons on a large scale.

Conventional, feed materials that are renewable replacements forpetroleum based base oils, process fluids, and white oils are usuallybased on vegetable oils or products derived from chemical modificationof vegetable oils such as diesters and polyol esters. These feedmaterials possess relatively higher reactivity that negatively affectsthe properties of the final product.

The method of the present invention is expected to efficiently producehigher purity hydrocarbons from renewable feed materials than othermethods of renewable hydrocarbon production. The hydrocarbon materialproduct of the present invention, White Alkanes, will possesshydrocarbons with most or all of the properties of white mineral oils.

As used herein, “renewable” (which may also be referred to as “renewablesources” or “renewable carbon”) may include polymerized vegetable oils,polymerized fatty acids, polymerized fatty acid esters, or a mixturethereof. The renewable carbon in the feed material may be chosen from,in part, from the polymerized vegetable oils, polymerized fatty acids,polymerized fatty acid esters, or a mixture thereof. Vegetable oils aregenerally trigylcerides (glycerol esters) which are esters of glyceroland various acid referred to as fatty acids that range from carbon chainlengths of C12-C24 and have additional functional groups such as doublebonds, or hydroxyl groups as in castor oil. Vegetable oils are producedin oilseed crops and fruits such as olive or palm, palm kernel andcoconut. Alternatively, the feed material is a naturally occurring oilor material containing 50% or more of unsaturated fatty acid componentsincluding mono-, di-, and tri-unsaturated hydrocarbon chains, with amajority of their fatty acids in the C16-C22 range. In general however,“renewable” or “renewable sources” or “renewable carbon” includes allcarbon sources that do not use fossil carbon from the geosphere. Fossilcarbon is generally petroleum—or coal, crude oil, and natural gas.Fossil carbon generally comes from decomposing plants and animals and isfound in the Earth's crust, and thus comes from the geosphere. Incontrast, renewable carbon comes from the biosphere, atmosphere, ortechnosphere—but not from the geosphere.

In one embodiment of the invention, vegetable oils containing shortchain length, unsaturated fatty acid chains are polymerized.Polymerization can be conducted by thermal treatment without or withpresence of oxygen (02) or air, and with or without a catalyst. Thesources may be triglycerides and fatty acid components chosen from oneor more natural sources such as: soy, canola, castor, corn, cottonseed,crambe, linseed, olive, peanut, rapeseed, safflower, sunflower, tall oilfatty acid, coconut, palm; oils derived from seeds, pulp, beans,legumes, rinds, pits or any part of an oil bearing fraction of theintended plant; animal fats or fish oils, or a mixture thereof. Theseoils contain 50% or more of unsaturated fatty acid components includingmono-, di-, and tri-unsaturated hydrocarbon chains, with a majority oftheir fatty acids in the C16-C22 range (C18 is typical for vegetableoil) that can be desirable for most applications, with final productcarbon chains of generally greater than C12 or C18 or C30 or C60 up toC100 being the target range after the process for the product.

Other naturally occurring oils or materials generally containingunsaturated hydrocarbon chains can also be used. Feed materialscontaining high levels of saturated hydrocarbon chains will give loweryields of the hydrocarbons usable as base oils, white oils, and processfluids, they will produce higher amount of renewable diesel. Forexample, animal fat, coconut oil, palm oil contain high level ofsaturation and will produce high amounts of renewable diesel fuel duringthe process.

The polymerized vegetable oil is hydro-decarboxylated, and/orhydro-deoxygenated, which will result in production of hydrocarbonssuitable for production of lubricants, or use in personal care productformulas, or as process oils.

Polymerized fatty acid and fatty acid esters can also be used as a feedin the hydro-decarboxylation, and/or hydro-deoxygenation step.

As an example, the process flow for using vegetable oil flows fromvegetable oil to polymerized vegetable oil using heat or heat and acatalyst. Then, the products of the first step are hydrogenated andtreated by different technologies to produce hydrocarbon materials,propane, and water. The hydrocarbon may or may not contain saturatedcarbon rings.

The resultant substance, White Alkane, has white oil quality. It iscreated generally from 50%400% renewable carbon and hydrocarbon basedmaterials, but in order to produce a higher quality product it ispreferable to use 80%-100% renewable carbon and hydrocarbon basedmaterials. The White Alkanes have the same inert hydrocarbon benefits asmineral oil and it is derived from natural ingredients per ISO 16128.

The resultant substance, White Alkane, has viscosities in a range (at40° C.) from 2 cSt to 60 cSt and higher. The preferred viscosities of 12cSt-70 SUS, 16 cSt-90 SUS, 40 cSt-209 SUS, or 60+ cSt-350+ SUS. WherecSt (or centistokes) is a unit of measure for viscosity is onemillimeter squared per second (1 cSt=1 mm²/s). While SUS (or SayboltUniversal Seconds) is the time in seconds for 60 milliliters (mL) of oilto flow through a standard orifice at a given temperature. cSt and SUSviscosity units are convertible between one another.

The produced renewable hydrocarbons will be used in the followingapplications where a renewable content is required, such as:

-   -   a. personal care products and pharma;    -   b. lubricants;    -   c. process fluids;    -   d. white oils;    -   e. components of agricultural products such as pesticides and        spray oils; and    -   f. any other use that may require hydrocarbon materials.

Unlike esterified fatty acids or purified vegetable oils, the proposedprocess produces “drop-in replacement” hydrocarbon materials andproducts of the same or better quality than mineral oils, white oils, orPAO.

The feed materials are selected with the highest possible content ofpolymerized hydrocarbon chains. During the method, it is desirable thathydrogen pressure 500-4000 psi and temperature 400° F.-800° F. and LHSV(LHSV is the liquid hourly space velocity, which is the ratio of liquidvolume flow per hour to catalyst volume. A system with a flow rate 2 cum/h and 1 cu m of catalyst would have an LHSV of 2.) of thehydrogenation process be 0.5-5 l/h. Further, the catalyst compositionfor hydrogenation should be Ni, Mo/Al₂O₃, or Ni, Co/Al₂O₃, Ni/Al₂O₃ orother metal based on catalyst support.

Hydrogenation can be conducted in several steps starting with milderconditions in order to decrease cracking reaction and increase the yieldof hydrocarbons with targeted hydrocarbon chains (C18 and higher). Forexample feed can first be treated at 20-4000 psi and temperature 200°F.-800° F. and LHSV of 0.5-5 l/h.

If acid dimers are used, a dilution maybe needed to reduce acid numberof the feed, and esterification or other chemical treatment to the dimermaybe beneficial to reduce acid number and increase the catalyststability. The produced materials will be hydrocarbons, that may or maynot contain saturated rings and traces of aromatics, and should have arange of carbon atoms from C12 to C100. A more likely embodiment woulduse C10 to C50, with C15 to C40 being the most common. The resultingmaterial is further purified by different methods in order to remove anyaromatic compounds, unreacted oxygenated hydrocarbons and produce WhiteAlkanes of desired properties.

The White Alkanes product is a white oil quality material, and meetssome or all of the following requirements: UV absorption, aromatics,color, readily carbonizable substances, and other white oilrequirements. The percentage of renewable carbon in the White Alkanes isbetween 50%-100%, although it is more desirable between 80%-100%, and ispreferably between 90%-100%. The starting feedstock is selected sourceshaving C12-C100 carbon chains, with significant portion of HC chainsbeing in C20 to C36 range.

In a substantial number of embodiments of the described method, aketonization step, an isomerization step, a transesterification stepfollowing polymerization, a transesterification step followingpolymerization or of the any polymerized vegetable oils, and/or ahydroisomerization step are unnecessary. Polymerizing the feed materialmay be accomplished using heat, or a catalyst, or heat and a catalyst,prior to hydro-decarboxylating the feed material, and prior tohydro-deoxygenating the feed material.

Feedstocks from the biosphere, such as plant fats, plant oils, plantwaxes, animal fats, animal oils, animal waxes, fish fats, fish oils,fish waxes, free fatty acids or fatty acids obtained by hydrolysis ofthe same, esters obtained by transesterification of the same, fatty acidalkyl esters obtained by esterification of alcohols with fatty acids ofthe same, fatty acid metal salts obtained by saponification of the same,alcohols and aldehydes obtained as reduction or hydrogenolysis productsof the same, fatty alcohols obtained by hydrolysis, transesterificationand pyrolysis from waxes of biological origin, anhydrides of fatty acidsfrom the same, and waste and recycled food grade fats and oils, do nottypically contain hydrocarbon chains longer than C22 and are notadvantageous for the described method.

In a substantial number of embodiments of the described method, glycerolis not produced, and thus separation is unnecessary. Likewise, theintermediate product of the present method does not have an iodine valueof 25 to 110, and a liquid fraction is not separated from theintermediate product of the present method.

Thus, the production of hydrocarbon material using renewable carbon asthe feed material includes selecting the feed material (which can comefrom many sources as described herein). The feed material is generallyalready polymerized, but if it is not, it can be polymerized as part ofthe method. The feed material is then subjected to a hydro treatment,which is a two-part step comprising hydro-decarboxylating andhydro-deoxygenating the feed material. These two (2) steps can result ina first intermediate.

The first intermediate can contain a mixture of molecules, or chemicals,and in some instances the first intermediate can have thecharacteristics sufficient to be classified as a White Alkane. The firstintermediate may be subjected to a separating step in which one or moreof the components, or different molecules, in the first intermediate canbe separated from the remainder—creating a second intermediate. Thetypical components that are separated and removed from either the firstintermediate or second intermediate may include: wax, linear alkanes,and/or light boiling alkanes. Several separation techniques can be usedon the first intermediate, including any one or more of: solventdewaxing, urea dewaxing, distilling, fractionating, fractionalcrystallization, or light fraction stripping. As an example, solventdewaxing processes can be used to remove wax from oils to give theproduct good fluidity characteristics at low temperatures.

The second intermediate may, in some instances, have the characteristicssufficient to be classified as a White Alkane. The first intermediate,or second intermediate, may also be subjected to a purification step, inwhich impurities are removed. The purifying step is accomplished by atleast one of: hydro finishing, applying sulfur trioxide, applying oleum,sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration.

It should be noted that a White Alkane may be produced after hydrotreatment, after hydro treatment and either separating, or purifying, orafter all three (3) steps hydro treatment, separating, and purifyinghave been completed. Additionally, the separating and purifying stepsmay be completed in any order.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 illustrates the method of the present invention.

FIG. 2 is a chart that illustrates selected characteristics ofvariations of the White Alkanes.

FIG. 3 is a schematic of a first embodiment of a production process ofthe White Alkanes.

FIG. 4 is a schematic of a second embodiment of a production process ofthe White Alkanes.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

Referring to the figures, FIG. 1 illustrates the steps that could beapplied in the present invention. 1. Refined vegetable oil and biodieselneed to be polymerized. Already polymerized materials can also be used.2. The initial hydro-de-oxygenation step produces a mixture ofhydrocarbons, typical conditions can be: hydrogen pressure 500-4000 psiand temperature 400° F.-800° F. and LHSV of the hydrogenation process be0.5-5 l/h over NiMo, CoMo, Ni, Co, or other metal Catalyst supported onAlumina, Silica silica-alumina or zeolite support or other hydrogenationcatalysts can be used. 3. If required, the hydrocarbons produced in thesecond step maybe separated by distillation or solvent dewaxing. Thisstep can produce hydrocarbons of different viscosity and coldtemperature properties. Fractions with atmospheric boiling temperatureup to 450° C. or higher can be separated if higher viscosity productsare desired. Separation of lower molecular weight linear alkanes ofC15-C18 range by distillation is also used here to improve the pourpoint of the resulting product. Solvent dewaxing is an alternativemethod for removing waxy alkanes, improving cold temperature properties,and increasing the viscosity of the final products. 4. In the productpurification step, hydro-finishing is used, typically run at 400°F.-700° F., 2000-7000 psi, 1.0 LHSV. Nickel catalyst or noble metal (forexample Pt, Pd) supported on Silica, Alumina, Silica-Alumina, Zeolitesupported catalysts are typically used. This step is desirable in orderto remove aromatic and heteroatom organic compounds (typically oxygencontaining aromatic compounds). The product purification step can alsobe performed by applying SO3, oleum, or sulfuric acid wash process. 5.If required, bauxite filtration is used as a final purification step.

The present invention uses a feed selection step. The feed selectionstep comprises selecting high natural content products, or feed,containing hydrocarbon chains with lengths from C10-C100. These may alsobe separated into more distinct groups where the feed material that thatcontains hydrocarbon chains with lengths of at least one of: C10 to C20,C20 to C30, C30 to C50, C50 to C70, C70 to C100. Generally, if higherviscosity product is desired, the feed material should contain longerhydrocarbon chains. The feed may be chosen from one, or a combination,of polymerized vegetable oils, polymerized fatty acids, and polymerizedfatty acid esters to create an intermediate product.

The intermediate product is treated with an initial hydrogenation step.In the initial hydrogenation step, unsaturated C═C bonds are saturatedthrough a reaction with hydrogen and oxygen atoms are converted to waterby reacting with hydrogen. As a part of the initial hydrogenation step,carbonyls present in the feed stock (a carbonyl group is a functionalgroup composed of a carbon atom double-bonded to an oxygen atom: C═O)can also be converted to CO2. Carbon atoms connected to oxygen aresaturated with hydrogen. Hydrocracking of the intermediate product intosmaller molecules may be a part of the initial hydrogenation andhydro-deoxygenation/decarboxylation step. The initial hydrogenation andthe hydro-deoxygenation/decarboxylation step(s) are one process.

Hydrocracking is a process by which the hydrocarbon molecules ofpetroleum are broken into simpler molecules by the addition of hydrogenunder high pressure and in the presence of a catalyst.

By controlling selectivity toward hydrocracking, the moleculardistribution and the viscosity of the resulting product is controlled.The initial hydrogenation may be done in two steps or over the layeredcatalyst bed in order to control the rate of hydrocracking. The layeredcatalyst bed consists of multiple catalysts, or reactors connected inseries.

An isomerization step may be applied in order to improve pour point ofthe product obtained in the initial hydrogenation step.

A product separation step can occur after initial hydrogenation, the mixof products can be separated by solvent dewaxing. Solvent dewaxingseparates waxy n-paraffins from liquid iso-paraffins andcyclo-paraffins. The solvent dewaxing improves the product pour point ofthe White Alkanes. Solvent dewaxing also removes light n-paraffins andincreases viscosity and increases flash point of the White Alkanes.Light fraction can be removed by stripping, this also improves flashpoint, pour point, and increases viscosity.

A fractionation step can be applied to the product where it isfractionated (distilled) in order to separate products of differentviscosity ranges. Removing of lower molecular weight linear alkanes(typically of C15-C18 range) by distillation is also used here forimproving the pour point of the resulting product.

A second stage purification step after the initial hydrotreatment stepor product separation steps where the intermediate product goes throughadditional purification by hydro-finishing. This second stagepurification helps produce White Alkanes with white oil quality. Thesecond stage purification step can accomplished by a treatment. Thetreatment may consist of at least one of: hydro finishing, applyingsulfur trioxide, applying oleum, or a sulfuric acid washing said secondintermediate product.

Finally, in a filtering step, the product may be filtered throughbauxite, palygorskite mineral, bentonite clay, kaolin clay, activatedcarbon or subjected to clay-gel extraction, in order to remove traceimpurities. The filtering step may also improve the appearance andclarity of the White Alkanes.

FIG. 2 is a chart that illustrates selected characteristics ofvariations of the White Alkanes. In this chart, WA stands for “WhiteAlkanes.” White Alkanes are renewable hydrocarbons. The viscosity rangeof the White Alkanes product should meet, but not be limited to:

-   -   a. US Pharmacopoeia USP <911> for Mineral Oil: 34.5-150.0 cSt;    -   b. Light Mineral Oil: 3.0-34.4 cSt;    -   c. European Pharmacopée Ph. EUR. <2.2.9>: P. Liquidium: 110-230        mPa-s (millipascal-second) (Dynamic viscosity is the resistance        to movement of one layer of a fluid over another and may be        measured using the Pascal second); and    -   d. P. Subliquidium: 25-80 mPa-s.

Other characteristics of the White Alkanes include, without limitation,a specific gravity/relative density that meets the requirements ofUnited States Pharmacopoeia per USP/NF <841>, and meets the requirementsof European Pharmacopoeia Ph. Eur. <2.2.5>. The acidity/alkalinity ofthe White Alkanes should meet the requirements of US PharmacopoeiaUSP/National Formulary (NF) <M02> and European Pharmacopoeia Ph. Eur.<M01>. The White Alkanes have no, or virtually no, remaining Sulfurcompounds, and meets the requirements of US Pharmacopoeia and FDA USP/NF<M04>. The White Alkanes also meet the requirements for ultraviolet (UV)absorption and Saybolt color found in 21 CFR 178.3620 (and for Sayboltcolor in the requirements of FDA test per ASTM D156).

FIG. 3 and FIG. 4 are schematics of sample processes of production ofthe White Alkanes. The final product, or White Alkanes, is the resultantof the inventive method. The White Alkanes is a hydrocarbon withrenewable carbon content of between than 50% to 100%, and containingnaphthenic and paraffinic carbons in a desired ratio. The White Alkanesis similar in quality to white oil and meets the requirements of thequality level set for white mineral oils per USP/NF Compendia, US Foodand Drug Administration CFR, European Pharmacopoeia Monographs. Somegrades may not meet the Solid paraffin requirements as they may not becritical for all applications. But, the White Alkanes meets therequirements for food additives of the Food and Drug Administration(FDA) per 21 CFR 172.878.

Byproducts of the described method may include wax n-paraffin C12-C100,propane or methane or ethane with 0 to 100% renewable carbon content, ordiesel or gasoline with 50-100% renewable carbon content.

When the terms “substantially,” “approximately,” “about,” or “generally”are used herein to modify a numeric value, range of numeric values, orlist numeric values, the term modifies each of the numerals. Unlessotherwise indicated, all numbers expressing quantities, units,percentages, and the like used in the present specification andassociated claims are to be understood as being modified in allinstances by the terms “approximately,” “about,” and “generally.” Asused herein, the term “approximately” encompasses +/−5 of each numericalvalue. For example, if the numerical value is “approximately 80,” thenit can be 80+/−5, equivalent to 75 to 85. As used herein, the term“about” encompasses +/−10 of each numerical value. For example, if thenumerical value is “about 80,” then it can be 80+/−10, equivalent to 70to 90. As used herein, the term “generally” encompasses +/−15 of eachnumerical value. For example, if the numerical value is “about 80,” thenit can be 80%+/−15, equivalent to 65 to 95. Accordingly, unlessindicated to the contrary, the numerical parameters (regardless of theunits) set forth in the following specification and attached claims areapproximations that may vary depending upon the desired propertiessought to be obtained by the exemplary embodiments described herein. Insome ranges, it is possible that some of the lower limits (as modified)may be greater than some of the upper limits (as modified), but oneskilled in the art will recognize that the selected subset will requirethe selection of an upper limit in excess of the selected lower limit.

At the very least, and not limiting the application of the doctrine ofequivalents to the scope of the claim, each numerical parameter shouldat least be construed in light of the number of reported significantdigits and by applying ordinary rounding techniques.

The terms “inhibiting” or “reducing” or any variation of these termsrefer to any measurable decrease, or complete inhibition, of a desiredresult. The terms “promote” or “increase” or any variation of theseterms includes any measurable increase, or completion, of a desiredresult.

The term “effective,” as that term is used in the specification and/orclaims, means adequate to accomplish a desired, expected, or intendedresult.

The terms “a” or “an” when used in conjunction with the term“comprising” in the claims and/or the specification may mean “one,” butit is also consistent with the meaning of “one or more,” “at least one,”and “one or more than one.”

The term “each” refers to each member of a set, or each member of asubset of a set.

The terms “comprising” (and any form of comprising, such as “comprise”and “comprises”), “having” (and any form of having, such as “have” and“has”), “including” (and any form of including, such as “includes” and“include”) or “containing” (and any form of containing, such as“contains” and “contain”) are inclusive or open-ended and do not excludeadditional, unrecited elements or method steps.

In interpreting the claims appended hereto, it is not intended that anyof the appended claims or claim elements invoke 35 U.S.C. 112(f) unlessthe words “means for” or “step for” are explicitly used in theparticular claim.

It should be understood that, although exemplary embodiments areillustrated in the figures and description, the principles of thepresent disclosure may be implemented using any number of techniques,whether currently known or not. The present disclosure should in no waybe limited to the exemplary implementations and techniques illustratedin the drawings and description herein. Thus, although the invention hasbeen described with reference to specific embodiments, this descriptionis not meant to be construed in a limited sense. Various embodiments mayinclude some, none, or all of the enumerated advantages. Variousmodifications of the disclosed embodiments, as well as alternativeembodiments of the inventions will become apparent to persons skilled inthe art upon the reference to the description of the invention. It is,therefore, contemplated that the appended claims will cover suchmodifications that fall within the scope of the invention.Modifications, additions, or omissions may be made to the systems,apparatuses, and methods described herein without departing from thescope of the disclosure. For example, the operations of the systems andapparatuses disclosed herein may be performed by more, fewer, or othercomponents in the methods described may include more, fewer, or othersteps. Additionally, steps may be performed in any suitable order.

We claim:
 1. A method of producing hydrocarbon material called a WhiteAlkane, wherein said White Alkane has the following properties: densityfrom 810-890 kg/m³ at 20° C. (using the standard test for density ASTMD-1298), viscosity from 3-240 cSt at 40° C. (using the standard test forviscosity ASTM D-445), pour point from −18-+3° C. (using the standardtest for pour point ASTM D-97), flash point from 115-290° C. (using thestandard test for flash point ASTM D-92), comprising: selecting a feedmaterial, wherein said feed material contains renewable carbon;hydro-decarboxylating said feed material; hydro-deoxygenating said feedmaterial; wherein a first intermediate is produced; and wherein saidfirst intermediate can be made up of a mixture of molecules.
 2. Themethod of claim 1, wherein said first intermediate is a White Alkane. 3.The method of claim 1, further comprising selecting said feed materialthat that contains hydrocarbon chains with lengths of at least one of:C10 to C20, C20 to C30, C30 to C50, C50 to C70, C70 to C100.
 4. Themethod of claim 1, further comprising polymerizing said feed materialusing heat, a catalyst, or heat and a catalyst, prior tohydro-decarboxylating said feed material, and prior tohydro-deoxygenating said feed material.
 5. The method of claim 1,wherein said feed material contains a renewable carbon that comes fromat least one of the biosphere, atmosphere, or technosphere.
 6. Themethod of claim 1, wherein said feed material renewable carbon is chosenfrom the group comprising: polymerized vegetable oils, polymerized fattyacids, polymerized fatty acid esters, triglycerides, diglycerides,monoglycerides, organic esters or a mixture thereof.
 7. The method ofclaim 1, wherein said feed material chosen from the group comprising:soy, canola, castor, corn, cottonseed, crambe, linseed, olive, peanut,rapeseed, safflower, sunflower, tall oil fatty acid, coconut, palm; oilsderived from seeds, pulp, beans, legumes, rinds, pits or any part of anoil bearing fraction of the intended plant; animal fats or fish oils, ora mixture thereof.
 8. The method of claim 1, wherein said feed materialis a naturally occurring oil or material containing 50% or more ofunsaturated fatty acid components including mono-, di-, andtri-unsaturated hydrocarbon chains, with a majority of their fatty acidsin the C16-C22 range.
 9. The method of claim 1, further comprising:separating said first intermediate into different components, andremoving wax, linear alkanes, or light boiling alkanes from said firstintermediate; wherein said separating step is accomplished by at leastone of: solvent dewaxing, urea dewaxing, distilling, fractionating,fractional crystallization, or light fraction stripping said firstintermediate product; and wherein a White Alkane is produced.
 10. Themethod of claim 3, further comprising: separating said firstintermediate into different components and removing wax, linear alkanes,or light boiling alkanes from said first intermediate; wherein saidseparating step is accomplished by at least one of: solvent dewaxing,urea dewaxing, distilling, fractionating, fractional crystallization, orlight fraction stripping said first intermediate product; and wherein asecond intermediate is produced.
 11. The method of claim 4, furthercomprising: separating said first intermediate into different componentsand removing wax, linear alkanes, or light boiling alkanes from saidfirst intermediate; wherein said separating step is accomplished by atleast one of: solvent dewaxing, urea dewaxing, distilling,fractionating, fractional crystallization, or light fraction strippingsaid first intermediate product; and wherein a second intermediate isproduced.
 12. The method of claim 5, further comprising: separating saidfirst intermediate into different components and removing wax, linearalkanes, or light boiling alkanes from said first intermediate; whereinsaid separating step is accomplished by at least one of: solventdewaxing, urea dewaxing, distilling, fractionating, fractionalcrystallization, or light fraction stripping said first intermediateproduct; and wherein a second intermediate is produced.
 13. The methodof claim 6, further comprising: separating said first intermediate intodifferent components and removing wax, linear alkanes, or light boilingalkanes from said first intermediate; wherein said separating step isaccomplished by at least one of: solvent dewaxing, urea dewaxing,distilling, fractionating, fractional crystallization, or light fractionstripping said first intermediate product; and wherein a secondintermediate is produced.
 14. The method of claim 7, further comprising:separating said first intermediate into different components andremoving wax, linear alkanes, or light boiling alkanes from said firstintermediate; wherein said separating step is accomplished by at leastone of: solvent dewaxing, urea dewaxing, distilling, fractionating,fractional crystallization, or light fraction stripping said firstintermediate product; and wherein a second intermediate is produced. 15.The method of claim 8, further comprising: separating said firstintermediate into different components and removing wax, linear alkanes,or light boiling alkanes from said first intermediate; wherein saidseparating step is accomplished by at least one of: solvent dewaxing,urea dewaxing, distilling, fractionating, fractional crystallization, orlight fraction stripping said first intermediate product; and wherein asecond intermediate is produced.
 16. The method of claim 3, furthercomprising: separating said first intermediate into different componentsand removing wax, linear alkanes, or light boiling alkanes from saidfirst intermediate; wherein said separating step is accomplished by atleast one of: solvent dewaxing, urea dewaxing, distilling,fractionating, fractional crystallization, or light fraction strippingsaid first intermediate product; and wherein a White Alkane is produced.17. The method of claim 4, further comprising: separating said firstintermediate into different components and removing wax, linear alkanes,or light boiling alkanes from said first intermediate; wherein saidseparating step is accomplished by at least one of: solvent dewaxing,urea dewaxing, distilling, fractionating, fractional crystallization, orlight fraction stripping said first intermediate product; and wherein aWhite Alkane is produced.
 18. The method of claim 5, further comprising:separating said first intermediate into different components andremoving wax, linear alkanes, or light boiling alkanes from said firstintermediate; wherein said separating step is accomplished by at leastone of: solvent dewaxing, urea dewaxing, distilling, fractionating,fractional crystallization, or light fraction stripping said firstintermediate product; and wherein a White Alkane is produced.
 19. Themethod of claim 6, further comprising: separating said firstintermediate into different components and removing wax, linear alkanes,or light boiling alkanes from said first intermediate; wherein saidseparating step is accomplished by at least one of: solvent dewaxing,urea dewaxing, distilling, fractionating, fractional crystallization, orlight fraction stripping said first intermediate product; and wherein aWhite Alkane is produced.
 20. The method of claim 7, further comprising:separating said first intermediate into different components andremoving wax, linear alkanes, or light boiling alkanes from said firstintermediate; wherein said separating step is accomplished by at leastone of: solvent dewaxing, urea dewaxing, distilling, fractionating,fractional crystallization, or light fraction stripping said firstintermediate product; and wherein a second intermediate White Alkane isproduced.
 21. The method of claim 8, further comprising: separating saidfirst intermediate into different components and removing wax, linearalkanes, or light boiling alkanes from said first intermediate; whereinsaid separating step is accomplished by at least one of: solventdewaxing, urea dewaxing, distilling, fractionating, fractionalcrystallization, or light fraction stripping said first intermediateproduct; and wherein a second intermediate White Alkane is produced. 22.The method of claim 10, further comprising: purifying said secondintermediate product; wherein said purifying step is accomplished by atleast one of: hydro finishing, applying sulfur trioxide, applying oleum,sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 23. The method of claim 11, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 24. The method of claim 12, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 25. The method of claim 13, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 26. The method of claim 14, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 27. The method of claim 15, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 28. The method of claim 1, further comprising: purifying saidsecond intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said second intermediateproduct; wherein said purifying causes impurities to be removed fromsaid second intermediate product; and wherein a White Alkane isproduced.
 29. The method of claim 1, further comprising: selecting saidfeed material that contains hydrocarbon chains with lengths of at leastone of: C10 to C20, C20 to C30, C30 to C50, C50 to C70, C70 to C100;purifying said first intermediate product; wherein said purifying stepis accomplished by at least one of: hydro finishing, applying sulfurtrioxide, applying oleum, sulfuric acid washing, bauxite filtration,clay-gel extraction, bentonite clay filtration, palygorskite mineralfiltration, kaolin clay filtration, or activated carbon filtration saidsecond intermediate product; wherein said purifying causes impurities tobe removed from said first intermediate product; and wherein a WhiteAlkane is produced.
 30. The method of claim 1, further comprising:polymerizing said feed material using heat, a catalyst, or heat and acatalyst, prior to hydro-decarboxylating said feed material, and priorto hydro-deoxygenating said feed material; purifying said firstintermediate product; wherein said purifying step is accomplished by atleast one of: hydro finishing, applying sulfur trioxide, applying oleum,sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said first intermediateproduct; wherein said purifying causes impurities to be removed fromsaid first intermediate product; and wherein a White Alkane is produced.31. The method of claim 1, further comprising: wherein said feedmaterial is a carbon source that comes from the biosphere, atmosphere,or technosphere; purifying said first intermediate product; wherein saidpurifying step is accomplished by at least one of: hydro finishing,applying sulfur trioxide, applying oleum, sulfuric acid washing, bauxitefiltration, clay-gel extraction, bentonite clay filtration, palygorskitemineral filtration, kaolin clay filtration, or activated carbonfiltration said first intermediate product; wherein said purifyingcauses impurities to be removed from said first intermediate product;and wherein a White Alkane is produced.
 32. The method of claim 1,further comprising: wherein said feed material chosen from the groupcomprising: polymerized vegetable oils, polymerized fatty acids, andpolymerized fatty acid esters, triglycerides, diglycerides,monoglycerides, organic esters or a mixture thereof; purifying saidfirst intermediate product; wherein said purifying step is accomplishedby at least one of: hydro finishing, applying sulfur trioxide, applyingoleum, sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said first intermediateproduct; wherein said purifying causes impurities to be removed fromsaid first intermediate product; and wherein a White Alkane is produced.33. The method of claim 1, further comprising: wherein said feedmaterial chosen from the group comprising: soy, canola, castor, corn,cottonseed, crambe, linseed, olive, peanut, rapeseed, safflower,sunflower, tall oil fatty acid, coconut, palm; oils derived from seeds,pulp, beans, legumes, rinds, pits or any part of an oil bearing fractionof the intended plant; animal fats or fish oils, or a mixture thereof;purifying said first intermediate product; wherein said purifying stepis accomplished by at least one of: hydro finishing, applying sulfurtrioxide, applying oleum, sulfuric acid washing, bauxite filtration,clay-gel extraction, bentonite clay filtration, palygorskite mineralfiltration, kaolin clay filtration, or activated carbon filtration saidfirst intermediate product; wherein said purifying causes impurities tobe removed from said first intermediate product; and wherein a WhiteAlkane is produced.
 34. The method of claim 1, further comprising:wherein said feed material is a naturally occurring oil or materialcontaining 50% or more of unsaturated fatty acid components includingmono-, di-, and tri-unsaturated hydrocarbon chains, with a majority oftheir fatty acids in the C16-C22 range; purifying said firstintermediate product; wherein said purifying step is accomplished by atleast one of: hydro finishing, applying sulfur trioxide, applying oleum,sulfuric acid washing, bauxite filtration, clay-gel extraction,bentonite clay filtration, palygorskite mineral filtration, kaolin clayfiltration, or activated carbon filtration said first intermediateproduct; wherein said purifying causes impurities to be removed fromsaid first intermediate product; and wherein a White Alkane is produced.35. A product, comprising: a White Alkane; wherein said White Alkane hascarbon chains generally in a range of C10 to C100; wherein said WhiteAlkane has a viscosity in a range from 2 cSt to 1000 cSt at 40° C.;wherein said White Alkane has a density from 810-890 kg/m³ at 20° C.(using the standard test for density ASTM D-1298); wherein said WhiteAlkane has a pour point from −18-+3° C. (using the standard test forpour point ASTM D-97); wherein said White Alkane has a flash point from115-290° C. (using the standard test for flash point ASTM D-92); whereinsaid White Alkane is made by a process comprising the steps of: choosinga feed material, wherein said feed material is a tri-glyceride,di-glyceride, mono-glyceride, organic acid ester, organic acid,naturally occurring oil or material containing 50% or more ofunsaturated fatty acid components including mono-, di-, andtri-unsaturated hydrocarbon chains, or a mixture of two or more of theabove; polymerizing said feed material using heat, a catalyst, or heatand a catalyst, prior to hydro-decarboxylating said feed material, andprior to hydro-deoxygenating said feed material; hydro-decarboxylatingsaid feed material; hydro-deoxygenating said feed material; separating acomponent from said feed material after hydro-decarboxylating said feedmaterial, and after hydro-deoxygenating said feed material; andpurifying said feed material after hydro-decarboxylating said feedmaterial, and after hydro-deoxygenating said feed material.
 36. Theproduct of claim 35, further comprising: wherein said separating step isaccomplished by at least one of: solvent dewaxing, urea dewaxing,distilling, fractionating, fractional crystallization, or light fractionstripping said first intermediate product; and wherein said purifyingstep is accomplished by at least one of: hydro finishing, applyingsulfur trioxide, applying oleum, sulfuric acid washing, bauxitefiltration, clay-gel extraction, bentonite clay filtration, palygorskitemineral filtration, kaolin clay filtration, or activated carbonfiltration said first intermediate product.
 37. The product of claim 36,wherein: said White Alkane is an inert, chemically stable compound; andsaid White Alkane is generally colorless, oily, almost tasteless,water-insoluble liquid, and said White Alkanes contains 50% or morerenewable carbon.